Catalyst system and process for the selective production of isoprenyl-alkylethers from isoprene

ABSTRACT

A catalyst system for the selective production of isoprenylalkylethers from isoprene is described, characterized by satisfying the following empirical formula 
     
         PdLxL&#39;y 
    
     where L is a phosphorated binder in the form of an organic derivative of trivalent phosphorous of type R 3  P or R 2  P[CH(R)] z  PR 2 , in which the substituents R, which can be identical or different, are either hydrogen atoms or alkyl, cycloalkyl, aryl, alkoxy, aryloxy, arylthio or arylalkyl groups, and in which z is a whole number between 1 and 5; 
     L&#39; is an easily displaceable binder chosen from dienes, olefins, anhydrides, diketones and nitriles; 
     x is a whole number between 0 and 4 and y is a whole number between 0 and 3, 
     in which system excess phosphorated compounds of R 3  P or R 2  P[CH(R)] z  PR 2  type may or may not be present.

This is a division of application Ser. No. 07/676,361, filed on Mar. 28,1991 now U.S. Pat. No. 5,120,868.

This invention relates to a catalyst system and its use in the selectiveproduction of isoprenyl-alkylethers by etherification of isoprene withmethanol or other alcohols under homogeneous liquid phase catalysis withtransition metal complexes.

Acid-catalyzed decomposition of ethers such as3-methyl-3-methoxy-1-butene, 3-methyl-1-methoxy-2-butene or1,3-dimethoxy-3-methylbutane is a known path for producing isoprene [DE2,213,701 (1972), J. O. Turner, Sun Res. and Dev. Co.].

It is also known to prepare said ethers by reacting isobutene withmethylal [U.S. Pat. No. 3,758,610 (1973)--J. O. Turner Sun Oil Co.].

By combining the two processes in one or more stages, a monomer such asisobutene can be converted into monomer such as isoprene.

It is further known to prepare the aforesaid ethers by acid-catalyzedaddition of an alcohol such as methanol to isoprene [U.S. Pat. No.2,922,822 (1960)--L. K. Beach, N. J. Westfield--Esso].

Combining this reaction with subsequent separation and decomposition ofthe ethers would seem to be an interesting procedure for removing andrecovering isoprene from hydrocarbon cuts which contain it in relativelylarge quantity, such as the C₅ fraction from steam cracking, and in thissense it could constitute a valid alternative to the conventionalextractive distillation procedure.

However such C₅ fractions contain not only isoprene but alsoconsiderable quantities of 2-methyl-1-butene and 2-methyl-2-butene whichas in the case of isoprene add methanol under acid catalysis, but give2-methoxy-2-methylbutane as the product, this being known commerciallyas TAME.

It is apparent that if a C₅ fraction from steam cracking is subjected toacid-catalyzed etherification a mixture of TAME and isoprenyl etherswould be obtained, this being difficult to separate, as is clear fromtheir boiling points:

    ______________________________________                                        3-methyl-3-methoxy-1-butene                                                                       B.P. (°C.)                                                                       83                                              TAME                "         86                                              3-methyl-1-methoxy-2-butene                                                                       "         104                                             ______________________________________                                    

It is also known that as in the case of isoprenyl ethers, TAMEdecomposes to give the starting olefins 2-methyl-1-butene and2-methyl-2-butene [FR 1,256,388 (1960)--Sinclair Res. Co.].

On decomposing the overall ether mixture a mixture of 2-methyl-1-buteneand 2-methyl-2-butene would therefore be obtained, from which it wouldbe difficult to isolate isoprene with sufficient purity because of thecloseness of their boiling points, as is apparent from the followingtable:

    ______________________________________                                        2-methyl-1-butene B.P. (°C.)                                                                       31                                                isoprene          "         34                                                2-methyl-2-butene "         39                                                ______________________________________                                    

It is further known that alcohols can be added to conjugate dienes inthe presence of salts or complexes of transition or post-transitionmetals.

The first catalysts of this type investigated were those based onRhCl₃.3H₂ O, with sufficiently selective formation of alkenyl-alkylethers [K. C. Dewhirst, J. Org. Chem. 32, (1967), 1297]. Later howeverthe importance of acidity in this type of system was observed [B. W.Taylor, Amer. Chem. Soc., Div. Petrochem. Prepr., 17 (2). (1972), B141].

In fact these catalysts also etherify simple olefins because of theiracid component, and cannot be used for selective etherification of1,3-dienes in the presence of an olefin stream. At the beginning of the1970s the main interest of researches was in directing the reaction of1,3-dienes with alcohols towards the production primarily ofdimerization or telomerization products. In this respect, if thereaction is conducted selectively on isoprene as a conjugate diene,terpene compounds could be obtained.

Reactions of this type have been studied mainly with catalysts based oncomplexes of Group VIII transition metals such as nickel and palladium[J. Tsuji, Adv. Organomet. Chem., 17 (1979) 141].

This reaction is catalyzed for example by Pd (0) complexes such asPd(PPh₃)₄ [DE 2,635,250 (1978), H. Jadamus, K. Diebel, Chemische WerkeHuels A. G.], and by phosphorated complexes of Pd (II) in the presenceor absence of bases [JP 75/154 201, (1975)--K. Sawatari, E.Tanaka--Yoshitomi Pharmaceutical Industries Ltd.].

However, the dimerization or telomerization products are not suitablesubstrates for the production of isoprene by decomposition.

Only recently has it been sought to direct this type of catalysistowards the selective production of alkenyl-alkylethers, and thusreducing all those processes which lead to chain elongation and hence tothe formation of dimers and/or telomers.

East German researchers have found that under suitable conditions thecatalyst system consisting of palladium (II) complexes, phosphoratedbinders and bases such as sodium methoxide can selectively produce thedesired ethers [DD 206,989 (1984)--H. Stegemann, H. Fuellbier, W. Gaube.E. Adler--VEB Chemisches Werk Militz].

This catalyst system suffers from various drawbacks.

The induction times are such as could cause reproducibility problems forthe catalyst system.

The bases make the catalyst system less selective in ethers, as alreadyobserved in the literature [W. Gaube, H. Stegemann, J. Prakt. Chem., 326(1984), 947].

In addition the presence of bases such as sodium methoxide can beharmful to the catalyst system, because it favours its reduction topalladium metal, which is inactive in this type of process. For thestated reasons, the selectivity of said system is not interesting froman industrial viewpoint.

The recently published U.S. Pat. No. 4,843,180 discloses a processdirected towards the synthesis of unsaturated ethers, in presence of acatalyst based on nickel (0) and phosphines as chelants, process whichprovides high conversions with average reaction times (from 5 to 22hours), using butadiene as starting diene. If using an hydrocarbonhaving a C number higher than 4 as starting diene, the same processpresents a considerable reduction of the conversion. A new catalyticsystem has now been surprisingly found, which possesses all the requiredcharacteristics for selectively etherifying isoprene in the presence ofa C5 fraction from steam cracking. This new system provides highconversions with, on average, low reaction times (from 1 to 6 hours).The new catalyst system comprises catalysts based on Pd (0) complexeswith phosphorated binders in the presence or absence of excessphosphorated compounds.

Palladium (0) complexes have been hitherto known to favour onlytelomerization reactions.

With this catalyst system there are no induction times, characteristicof the system formed from palladium (II) complexes in the presence ofphosphorated binders.

This new catalytic system also differs by having very high activity andselectivity in the production of isoprenyl-alkylethers and of leavingall olefins completely unaltered, including those having a double bondin the tertiary position.

This characteristic is not sufficiently available either with rhodiumcatalysts (which are not selective in the presence of simple olefins) orwith the Pd (0) telomerization catalyst complexes, which are unable toproduce alkenyl-alkylethers with the monomer alkenyl group.

The catalyst system of the present invention for producingisoprenyl-alkylethers from isoprene (such as contained in C₅ hydrocarboncuts) is characterised by satisfying the following empirical formula

    PdLxL'y

where L is a phosphorated binder in the form of an organic derivative oftrivalent phosphorus of type R₃ P or R₂ P[CH(R)]_(z) PR₂, in which thesubstituents R, which can be identical or different, are ether hydrogenatoms or alkyl, cycloalkyl, aryl, alkoxy, aryloxy, arylthio or arylalkylgroups containing preferably between 1 and 10 carbon atoms, and in whichz is a whole number between 1 and 5; L' is an easily displaceable binderchosen from dienes (in particular butadiene, isoprene and1,5-cyclooctadiene), olefins (in particular ethylene), anhydrides (inparticular maleic anhydride), diketones (in particulardibenzylideneacetone [dba]), and nitriles (in particular acetonitrileand benzonitrile); x is a whole number between 0 and 4 and y is a wholenumber between 0 and 3, the sum of x+y being greater than or equal to 2.The aryl groups of part of the substituents R can also be substituted atthe ring by other halogen or alkoxy groups.

The phosphorated binder L of R₃ P type is chosen preferably fromtrialkylphosphines such as tri-n-butylphosphine or triethylphosphine,and alkyl-aryl phosphines such as di-n-butylphenylphosphine. Thephosphorate binder L of R₂ P[CH(R)]_(z) PR₂ type is chosen preferablyfrom those in which z is 4, such as 1,4-bis(diphenyl-phosphino)butane(DPPB).

As above mentioned the catalytic system of the present invention cancomprise excess phosphorated compounds of R₃ P or R₂ P[CH(R)]_(z) PR₂types, wherein the substituents R, which can be identical or different,are the same groups above mentioned for the binder L. The said excessphosphorated compounds are chosen preferably from tri-n-butyl-phosphine,triethylphosphine, di-n-butylphenylphosphine and1,4-bis(diphenyl-phosphino)butane (DPPB).

The aforesaid palladium complexes with phosphorated binders can beprepared by the methods already exhaustively described in the literature[such as the preparation of Pd(Pn--Bu₃)₄ and Pd(PPh₃)₄ (where Bu=butyland Ph=phenyl) is described by W. Kutan, A. Musco, in Inorg. Chem. Acta12 (1975), 183, and by D. R. Coulson in Inorg. Synth. 13 (1972), 120].

The present invention further provides a process for producingisoprenyl-alkylethers from alcohols and isoprene present in a C₅ streamfrom which cyclopentadiene has been removed preferably by thermaldimerization and most of the linear dienes (piperylene) have beenremoved preferably by fractional distillation.

The selectivity of the reaction towards isoprene rather than towardspiperylene is further increased in the etherification reaction becausethe catalyst system when operating under the indicated preferredconditions selectively etherifies the isoprene.

Said process consists of reacting the C₅ fraction obtained in thismanner with alcohols in the presence of the aforedescribed catalystsystem.

The alcohol is chosen preferably from C₁ -C₁₀ alcohols and morepreferably from methanol and ethanol.

The catalyst system operates in the absence of additional solvent as theC₅ fraction is in itself a good solvent.

However additional solvents can if necessary be used. These can consistfor example of non-conjugate olefinic substrates, paraffins, aromatichydrocarbons, heavier alcohols such as isopropanol, or ethers, as canthe reaction products themselves. If operating with one or moresolvents, the concentration of the catalyst system can vary preferablybetween 0.0001 and 1 and more preferably between 0.001 and 0.1 molar forthe palladium (0) complex and between 0 and 10 and more preferablybetween 0 and 1 molar for the added C₅ phosphorated binder.

The isoprene/Pd molar ratio can vary preferably between 10 and 1000 andmore preferably between 50 and 500, whereas the alcohol/isoprene molarratio can vary preferably between 1 and 100 and more preferably between5 and 50.

The reaction temperature is preferably less than 150° C. and morepreferably between 50° and 130° C.

The operating pressure can vary between 0.1 MPa and 10 MPa, but morepreferably is represented by the vapour pressure of the components ofthe reaction mixture.

When operating under the indicated preferred conditions, isopreneconversions exceeding 90% have been obtained, with initial rates ofabout 0.1 s⁻¹ (moles of isoprene converted per mole of palladium persecond), and a very high isoprenyl-alkylether selectivity (between 80and 100%).

The by-products obtained are generally dimers and a minimum of trimers,isoprene or telomers of the diene obtained by addition of the alcohol tothe dimers.

The following examples are given to better illustrate the invention, butwithout representing a limitation thereon. (In the examples the statedpercentages are molar).

EXAMPLE 1

This example illustrates the use of the catalyst of the presentinvention in reacting a C₅ stream with methanol at 110° C. in a batchreactor.

0.27 mmoles of Pd(Pn--Bu₃)₄, 2.19 mmoles of Pn--Bu₃, 820 mmoles ofmethanol and 144.3 mmoles of a C₅ hydrocarbon mixture are mixed in a 100ml autoclave with a magnetic stirrer. The C₅ hydrocarbon mixture has thefollowing composition: inerts 54.7%; isoamylenes 11.7%; isoprene 32.4%;piperylene (trans+cis) 0.5%; cyclopentadiene 0.7%. This feedstock wasobtained from a further feedstock originating from steam cracking afterthermal treatment to eliminate the cyclopentadiene and fractionaldistillation to eliminate the linear dienes.

A typical composition of feedstock from steam cracking is as follows:inerts 35.0%; isoamylenes 6.3%; isoprene 18.7%; piperylene 16.3%;cyclopentadiene 23.3%; benzene 0.4%. The inerts consist of saturatedhydrocarbons and a mixture of linear pentenes and cyclopentene.

The operation is carried out under a nitrogen atmosphere, heating to110° C.

Operating in this manner an isoprene conversion of 97% was obtainedafter 3 hours, with an isoprenyl-methylethers selectivity of 86% (yield83%), a piperylene conversion of 87% with a pentenyl-methylethersselectivity of 98% (yield 85%), and a cyclopentadiene conversion of 57%with a cyclopentenyl-methylethers selectivity of 8% (yield 4%, theremainder being dicyclopentadiene).

None of the other mixture components (including the isoamylenes) undergoany reaction.

The isoprenyl ethers selectivity within the C₅ ether fraction exceeds98%.

EXAMPLE 2

This example shows how the selectivity of the catalyst system forisopropene compared with piperylene and cyclopentadiene can be increasedby altering the experimental conditions.

The procedure is carried out under the same conditions as in Example 1but using a temperature of 100° C.

Operating in this manner an isoprene conversion of 40% was obtainedafter 6 hours, with an isoprenyl-methylethers selectivity of 89% (yield36%), a piperylene (cis+trans) conversion of 8% with apentenyl-methylether selectivity of 99% (yield 8%), and acyclopentadiene conversion of 15% with a cyclopentenyl-methylethersselectivity of 18% (yield 3%).

Again, none of the other mixture components undergo any reaction. Theisoprenyl ethers selectivity within the C₅ ether fraction exceeds 99%.

EXAMPLE 3

This example shows how selective etherification of isoprene can beconducted in the presence of an added solvent.

The procedure of Example 1 is followed, but feeding the autoclave with0.137 mmoles of Pd(Pn--Bu₃)₄, 1.096 mmoles of Pn--Bu₃, 20.6 mmoles ofisoprene, 411 mmoles of methanol and 40 ml of anhydrous toluene as theadded solvent.

Operating in this manner an isoprene conversion of 72% was obtainedafter one hour of reaction, with a methyl-isoprenyl ethers selectivityof 89% and yield of 64%.

EXAMPLE 4

This example shows how an active and selective catalyst system is stillobtained under mild conditions.

The conditions of Example 3 are followed, but using a temperature of 80°C. and 0.18 mmoles of tri-n-butylphosphine.

A conversion of 74% was obtained after one hour of reaction, with amethyl-isoprenyl ethers selectivity of 90% and yield of 67%.

EXAMPLE 5

This example shows that the catalyst system also gives high performancewith other phosphines of R₃ P type.

The conditions of Example 3 are followed, but the catalyst systemconsists of Pd(Pn--Bu₂ Ph)₄ (0.137 mmoles) in the presence of 1.10mmoles of Pn--Bu₂ Ph.

A conversion of 83% was obtained after 6 hours of reaction, with amethyl-isoprenyl ethers selectivity of 85% and yield of 71%.

EXAMPLE 6

This example shows that good performance of the catalyst system is alsoobtained with other phosphines of R₂ P[CH(R)]_(z) PR₂ type. Theconditions of Example 3 are followed but with a temperature of 60° C.and a catalyst system consisting of Pd(DPPB)₂ (0.137 mmoles) in thepresence of 0.55 mmoles of DPPB.

A conversion of 12% was obtained after 6 hours of reaction, with amethyl-isoprenyl ethers selectivity of 85% and yield of 10%.

EXAMPLE 7

This example shows that moderate performance of the catalyst system isobtained with a complex of the PdL_(x) L'_(y) type (where x=0, y=2),such as Pd(dba)₂.

The conditions of Example 3 are followed but with a temperature of 100°C. and a catalyst system consisting of Pd(dba)₂ (0.137 mmoles) in thepresence of 1.65 mmoles of nBu₃ P.

A conversion of 5% was obtained after 3 hours of reaction, with amethyl-isoprenyl ethers selectivity of 85% and yield of 4%.

EXAMPLE 8 (Comparative)

This example shows that in our invention the yields of desired productsare maximized for equal experimental conditions, compared with thatclaimed previously in the literature.

The method and experimental conditions described in Example 4 arefollowed.

The catalyst system is prepared as described in the patent DD 206,989,and consists of 0.07 mmoles of [Pd(C₃ H₅)Cl]₂, 0.82 mmoles of PnBu₃ and0.21 mmoles of CH₃ ONa.

After one hour of reaction an isoprene conversion of 57% was obtainedwith a methyl-isoprenyl-ethers selectivity of 65% and a yield of 37%.

EXAMPLE 9 (Comparative)

This example shows that in our invention the yields of desired productsare maximized for equal experimental conditions, compared with thatpreviously described in the literature, even if other phosphoratedbinders are present.

The conditions described in Example 5 are followed.

The catalyst system is prepared as described in the patent DD 206,989,and consists of 0.07 mmoles of [Pd(C₃ H₅)Cl]₂, 1.64 mmoles of Pn--Bu₂ Phand 0.21 mmoles of CH₃ ONa.

After 6 hours of reaction an isoprene conversion of 83% was obtainedwith a methyl-isoprenyl ethers selectivity of 72% and yield of 60%.

EXAMPLE 10 (Comparative)

This example shows that it is not possible to conduct selectiveetherification of isoprene in the presence of an olefinic stream using arhodium catalyst system [see K. C. Dewhirst, J. Org. Chem. 32, (1967),1297].

The procedure of Example 1 is followed. 0.57 mmoles of RhCl₃ ·3H₂ O,14.7 mmoles of isoprene, 14.7 mmoles of 2-methyl-1-butene and 750 mmolesof methanol are however fed into the autoclave at 60° C.

After 6 hours the isoprene conversion was 87%, with a methylisoprenylethers selectivity of 89% (yield 77%).

A part of the 2-methyl-1-butene isomerizes to 2-methyl-2-butene, whichis also converted to TAME.

The TAME yield from both isoamylenes is 51%.

We claim:
 1. A process for the selective production ofisoprenyl-alkylethers from isoprene present in a C₅ stream from whichthe cyclopentadiene and most of the linear dienes (piperylene) have beenremoved which comprises: reacting the C₅ fraction obtained in saidmanner with alcohols in the presence of a catalyst system satisfying thefollowing empirical formula

    PdL.sub.x L'.sub.y

where L is a phosphorated binder in the form of an organic derivative oftrivalent phosphorus of type R₃ P or R₂ P[CH(R)]_(z) PR₂, in which thesubstituents R, which can be identical or different, are either hydrogenatoms or alkyl, cycloalkyl, aryl, alkoxy, aryloxy, arylthio or arylalkylgroups, and in which z is a whole number between 1 and 5; L' is aneasily displaceable binder chosen from dienes, olefins, anhydrides,diketones and nitriles; x is a whole number between 0 and 4 and y is awhole number between 0 and 3, the sum of x+y being greater than or equalto
 2. 2. A process as claimed in claim 1, wherein excess phosphoratedcompounds of R₃ P or R₂ P[CH(R)]_(z) PR₂ type are present.
 3. A processas claimed in claim 1, wherein the isoprene/Pd molar ratio variesbetween 10 and 1000 and the alcohol/isoprene molar ratio varies between1 and
 100. 4. A process as claimed in claim 3, wherein the isoprene/Pdmolar ratio varies between 50 and 500 and the alcohol/isoprene molarratio varies between 5 and
 50. 5. A process as claimed in claim 1 andpossibly 2, wherein the catalyst system operates in the presence of oneor more added solvents, with a molar concentration of between 0.0001 and1 for the palladium complex (PdL_(x) L'_(y)) and between 0 and 10 forthe excess added phosphorated compound.
 6. A process as claimed in claim5, wherein the molar concentration of the palladium complex is between0.001 and 0.1 and for the excess added phosphorated compound is between0 and
 1. 7. A process as claimed in claim 1, wherein the reaction isconducted at a temperature of less than 150° C. and at a pressure ofbetween 0.1 and 10 MPa.
 8. A process as claimed in claim 7, wherein thetemperature is between 50° and 130° C.